Hydro-oily emulsion burning process

ABSTRACT

A burning process comprising the steps of emulsifying fuel oil with water and aerating the emulsion in a mixing tank until there is a substantial reduction of its density. The emulsion is then stabilized in a resting tank under adequate temperature and pressure conditions for maintaining an deaerating the emulsion. The stabilized emulsion is conducted to a burner nozzle where it is pulverized into particles by means of abrupt decompression in an environment poor of air.

TECHNICAL FIELD

The present invention is applicable to a process for burning an emulsionof water and a fuel oil, with a high heat-generating yield, includingthe procedures to obtain and stabilize this emulsion, under adequateconditions for the proposed burning process.

BACKGROUND ART

The optimization of burning together with the inherent economy of fuelobtained, has been, over the years, a permanent concern of thoseresponsible for manufacturing and/or operating heat-generating units, aswell as of the suppliers of fuels, that is, the distributors of oilproducts. By this token, numerous papers have been developed by theinvolved parties, as well as in the field of emulsifying fuel oil withwater. However, whether due to the operational sequence, or whether dueto the process conditions adopted, in spite of the high degree oftechnological development reached in heat-generating equipment,relatively little progress has been reached in the last two decades interms of fuel economy, whereas the most relevant results obtained do nomore pertain changes in the fuel itself, but are due to a more accuratecontrol of burning, obtained through the aid of computer technology.Concerning the techniques of emulsifying fuel oil and water, instantemulsification, emulsion additivation, as well an endless number ofmechanical and/or chemical modification processes were developed aimingat, among other parameters, the possibility of adding, under stableconditions, larger amounts of water to emulsions, in order to obtainyields of heat at least equal to fuel oil in terms of mixture with air.

However, the most efficient known processes for hydro- emulsifying fueloil have provided gains in heat yields at an average of about 3%, or ata maximum between around 5 and 8%, if compared with the yield by burninga perfectly adjusted air/oil mixture.

Even for those who are not familiar with the art, it must seemintuitively evident that, if adequately used, the ideal adjuvant of fueloil in terms of costs is water.

By this token, and taking as a basis the knowledge of the art thenavailable, the applicant, for the first time, decided to developpersevering studies with the purpose of optimizing process conditionsrelated to each operational stage of hydro-emulsification. The recordspresented, for the first time, references to improved stabilitycharacteristics and heat value of hydro-oily emulsions for burning inburner nozzles of heat-generating equipment, by simply adjusting time,pressure and temperature parameters.

Although describing a hydro-oily solution burning process, including thesteps of emulsifying, deaerating, conducting and pulverizing theemulsion, the most recent state of the art does not get to determine, ina clear manner, the basic conditions for the different steps in order toreach the intended results and the reactions of imperative occurrenceduring the pulverization steps, for it to be possible to reach aneconomy in different experiments.

Thus, the present invention has the basic object to provide a hydro-oilyemulsion burning process at the burner nozzle of a heat-generatingequipment, with a high heat yield and low implementation cost.

It is also an object of the present invention to provide a hydro-oilyemulsion burning process, as described above, including a procedure forobtention and stabilization of the referred hydro-oily emulsion.

It is a further object of the current invention to provide a hydro-oilyemulsion burning process, as described above, in which the referredemulsion encloses a water concentration markedly superior to the usualwater concentrations obtained, associated to an equally superior heatvalue.

DISCLOSURE OF THE INVENTION

These and other objectives and advantages of the current invention arereached through the provision of a hydro-oily emulsion burning process,of the type composed of water and fuel oil, to be burnt at the burnernozzle of a heat-generating equipment, including the steps of:emulsifying and aerating water and fuel oil, by means of agitation in amixing tank, the water being maintained at a minimum temperature of 20°C.±2° C. and the fuel oil at a maximum temperature lower than that ofvaporization of water and at an adequate working pressure to facilitatethe desired emulsification, the concentration of water in the emulsionbeing calculated to react stoichiometrically during combustion,producing hydrogen and carbon dioxide, said emulsion being maintained ata temperature sufficient to permit an interfacial tension between fueloil and water and air, at compatible levels to stabilize the emulsionand at a pressure corresponding to a temperature of saturated watersteam substantially higher than the temperature of the emulsion, so thatthe latter presents all the water maintained in the form of droplets ofaround 1 to 10 microns, uniformly dispersed, together with micro bubblesof air, in the fuel oil, the speed and time of agitation beingdetermined in order that the aerated emulsion obtained presents specificgravity around 20±5% lower than the deaerated hydro-oily emulsion;stabilizing the aerated emulsion in a rest tank, maintained undertemperature and pressure conditions that ensure the required ratio ofinterfacial tension between water and oil and maintenance of the waterconcentration , for a period of time required and sufficient topractically fully deaerate said emulsion; conducting the deaerated andstabilized emulsion to a burner nozzle, maintaining the emulsionconduction temperature between a maximum value, corresponding to that ofa saturated steam pressure mandatorily lower than the emulsionconduction pressure, and a minimum value corresponding to the minimumsensible heat stored, capable of vaporizing a minimum quantity of waterunder an abrupt pressure drop condition, by pulverization at the burnernozzle, the pressure of conduction of the emulsion being maintainedwithin the operating values required by the burner; pulverizing theemulsion through the burner, in uniform particles of around 20 to 150microns, each particle comprising plurality of said water droplets inthe emulsion, surrounded by a film of oil, said pulverization beingeffected so as to provoke an abrupt depressurization of the emulsion,sufficient to cause the instantaneous vaporization (flashing) of part ofthe water from the droplets and the consequent disintegration of theparticles of the pulverized emulsion, said pulverization being effectedin an environment sufficiently poor of air in order to avoid directformation of carbon dioxide and to convey the following reactions:

a partial combustion of the fuel oil with part of the oxygen availablein the pulverization environment, forming carbon monoxide and releasingheat;

b reduction of water vaporized during the abrupt depressurization of theemulsion, by means of a stoichiometric amount of part of the referredcarbon monoxide, forming carbon dioxide and hydrogen and releasing heat,

c oxidation of hydrogen, from reaction b, with the remaining oxygenavailable in the pulverization environment, forming hiperheated watersteam at burner flame temperature,

d vaporization of water, remaining in the droplets, by the heat producedin reactions a and b;

e reduction of water vaporized in reaction d by the carbon monoxideremaining from step a, through chain reactions identical to reactions band c, so as to provoke the total combustion (burning) of the oil.

The innovation presented by the proposed invention translates into aprocess of burning a hydro-oily emulsion of fuel oil and water,including the required procedures for obtaining and stabilizing thespecified emulsion, which incorporates a high quantity of water inrelation to those quantities conventionally used and which also presentsan increased heat value. In practical terms, the proposed processpresents, among others, the following advantages, providing the userconsumption reductions to the order of 25%; emulsions with a highincorporation of water, which participates chemically of highlyexothermal reactions and contributes, therefore, positively to the heatbalance of all the stages of the process; based on the micropulverization of fuel and the high temperature of this burning processpractically the entire solid particulate material residues areeliminated, that is, the burning is practically complete and perfect,thus reducing to a minimum stoppages and expenses with maintenance suchas nozzle cleaning, filters and others.

BRIEF DESCRIPTION OF THE DRAWINGS

Next, the invention is described with reference to the attacheddrawings, wherein:

FIG. 1 represents a schematic view of an installation for emulsifying,stabilizing and burning a hydro-oily emulsion, according to the proposedprocess;

FIG. 2 represents a schematic view of the flame profile produced by theproposed process, presenting the described flame regions as well as thetypes of chemical reactions occurring in these regions;

FIG. 3 represents an enlarged view of the flashing region of FIG. 2,presenting the particulated emulsion, before suffering the flashingphenomenon; and

FIG. 4 represents an enlarged view of an emulsion particle, according toFIG. 3.

BEST MODE FOR CARRYING OUT THE INVENTION

According to the figures described, the hydro-oily emulsion burningprocess, of the type composed by fuel oil and water, to be burned at theburner nozzle of a heat-generating equipment, comprises the stages of:preparing the oil and water emulsifying and aerating oil and water,stabilizing and deaerating the emulsion formed, and pulverizing thestabilized emulsion, including its burning.

The step of forming the emulsion consists in agitating, preferablymechanically and at 700 rpm, during a pre-determined period, normallyvarying around 2 and 3 minutes, in a heated and eventually pressurizedmixing tank 10, a pre-heated fuel oil at a temperature varying,depending on the viscosity of the oil used, between about 50° and 200°C., with water at a maximum temperature lower than that of vaporizationat working pressure and minimum of 20° C.±2° C. and preferablydemineralized or softened, such water generally being admitted in themixing tank 10 as a jet tangent to the wall of the latter and along thesame course as the agitation of the oil, and in a predetermined amountdepending on the viscosity of the oil utilized and the stoichiometriccondition required for the combustion reaction, to be described ahead.The emulsion formed generally presents a composition containing between55 and 70% fuel oil and between 45 and 30% water, and a temperatureafter beating between 70° and 90° C. in a non-pressurized tank and above90° C. in a pressurized mixing tank.

The step described above is generally effected at atmospheric pressurefor oils presenting viscosities lower than 100 cst (130° C.); above thisviscosity, emulsification is processed under pressure, generally varyingbetween 2 and 10 kgf/cm², in order to avoid losses of emulsion waterthrough evaporation, because of the high temperature required to liquefythe fuel oil. In other words, we can say that the pressure in the mixingtank should correspond to a vaporization temperature of water,substantially higher than that of the emulsion.

Since, during the process of agitating a liquid, aeration occurs at aproportional rate to the speed and time of agitation, it is important tomaintain the above mentioned speed, preferably around 700 rpm, during aperiod of time generally between 2 to 3 minutes, so as to control thevolume of air absorbed, since this was determined experimentally as theideal volume of air (or of inert gas, when the high temperature of fueloil is favorable for its oxidation), around 20% of the total volume ofwater and oil, that is, such a volume that will reduce the specificgravity of the emulsion by around 20%±5%. Under the conditions describedabove, an emulsion is produced whereby the water droplets with diametersof around 1 to 10 microns are evenly dispersed in oil, and where saidemulsion is permeated with micro bubbles of air, also evenlydistributed.

The micro bubbles of air, as well as the water droplets, as distributed,are fully surrounded by fuel oil, once the interfacial tension of thelatter with the first ones is smaller than the interfacial tensionbetween the first. In this manner, the total interfacial surface of oilcorresponds to the summing up of the external surfaces of the waterdroplets and of the micro bubbles of air, or yet, there is full contactbetween the fuel oil and the two last ones in the formed emulsion.

The formed emulsion is duly aerated and transferred, through pump 11 andrespective tubing 12, to a rest tank 20, where it should remain for aperiod of around 6 to 12 hours, under suitable conditions to maintainstable such an emulsion, conditions which should also be based on itsconcentration, oil viscosity and temperature required to maintain thedesired ratio of the interfacial tension within the latter.

Pressurization will be utilized in this stage when the oil viscositygoes over 225 cst (130° C.), since such an oil requires, in order toflow sufficiently, high temperatures so that under atmospheric pressureconditions, they are able to promote evaporation of water from theemulsion.

During the rest tank step, as described above, the deaeration of theemulsion occurs and, with the displacement of the micro bubbles of air,occupation of its space by the fuel oil occurs, contributing to aperfect and uniform involvement of the droplets by the latter. Thedeaeration operation of said emulsion is equally important in itsstabilization step, due to the fact that air is a poor heat conveyor,therefore, the micro bubbles of air are acting as a thermal barrier.Their elimination, therefore, will permit a perfect distribution of heatthroughout the whole emulsion.

In cases of non-pressurization of the rest tank 20, that is, when thefuel oil utilized presents viscosity up to 225 cst (130° C.), thedeaeration can be processed through ventilation on the surface of theemulsion, obtained by means of circulation of air through air intakevents 21, the air taken in being re-expelled by a chimney 22, with itsheight dimensioned so as to allow drawing the air out through athermosiphon mechanism, thus avoiding formation of negative pressures onthe surface of the emulsion, which would impair the stability of thesame.

Following stabilization, the emulsion should go through a critical stepof the process in question, which is, it being conducted from the resttank 20 to the burner nozzle 30. This operation, generally effectedthrough pump 25 and respective piping 26, should be effected in such amanner as to ensure maintaining the stability of said emulsion, thusavoiding the separation of water, be it in the form of steam, be it inthe form of liquid. This condition is obtained by pumping the emulsionto a heater 40, where it will be heated up to such a temperature whichwill correspond to that of a water saturated steam pressure, preferablyat around 15% lower than the pressure to which said emulsion is beingsubject during conduction. Higher temperatures would lead to separationof water by evaporation; lower temperatures would hinder transportationof the emulsion due to its increased viscosity.

The hydro-oily emulsion, duly stabilized, pressurized and heated, isthen pumped to burner nozzle 30, to be pulverized into an environmentsufficiently poor of air in order to avoid forming carbon dioxidedirectly, that is, to conduct only a partial combustion of thepulverized fuel oil. The emulsion is, pulverized in such a way as toform substantially spherical particles 50, presenting diameters ofaround 70 to 100 microns and, each one, defined by a mass of waterdroplets 51, finely dispersed, and surrounded by a film of oil 52.

The above described particles 50, when leaving burner nozzle 30 at apre-determined temperature, generally between around 120° and 250° C.,suffer an abrupt depressurization, producing instant vaporization,flashing of part of the water of the droplets (for example, around 5% to20% of the mass of water) and, consequently, one micro explosion of eachparticle, disintegrating the oil films and provoking the formation of afine mist by enhancement of the pulverizing effect. Next, the pulverizedemulsion, as described above, goes on to the burning phase. To betterunderstand the phenomenon, the flame area will be subdivided into threedistinct regions: a flashing region, a flame formation region and theflame region itself (see FIG. 2).

At the flashing region, as described above, hiperpulverization of thefuel oil and vaporization of part of the water droplets of the emulsionoccur. At the flame formation, basically, the reactions of the productsgenerated from flashing, which are, the decomposition of fuel oil,completed by the radiation heat of the flame, the partial combustion ofthe decomposed oil mist, followed by the reduction of part of thevaporized water with a portion of CO, formed by the previous reactionoccur.

The reaction of partial combustion of fuel oil from the flash, which issubstantially exothermic, occurs at the ignition temperature of such anoil, with a portion of poor air admitted together with the emulsion atthe burner nozzle, as follows:

    C+1/2O.sub.2 →CO ΔH=-943 kcal/kg of CO

Next, part of the water vaporized through flashing, corresponding, asalready mentioned, to around 10% of the total water that composes theemulsion, suffers a reduction by a stoichiometric quantity of the carbonmonoxide formed in the previous reaction, as follows:

    CO+H.sub.2 O(v)→CO.sub.2 +H.sub.2 ΔH=-546 kcal/Kg of H.sub.2 O(v)

A chain reaction of vaporization and reduction of the water remainingfrom the emulsion will occur at the flame formation region, whereas theoxidation of hydrogen formed from said chain reaction will occur as fromits generation, until the flame region.

The oxidation of the hydrogen originated from the field oil decomposedduring flashing, begins at the flame forming region. The oxidation ofremaining carbon monoxide, not used for the reduction of steamed water,probably occurs immediately after the conclusion of the reductionreactions, at the intermediate zone.

Hydrogen formed from the reduction of steam coming from flashing isoxidized in the presence of the remaining, non reacted, portion of thequantity of poor air (oxygen) available in the pulverizationenvironment, forming steam in the condition of gas, at flametemperature, through a strongly exothermic reaction.

    H.sub.2 +1/2O.sub.2 →H.sub.2 O(v) ΔH=-3,211 kcal/kg of H.sub.2 O(v)

Water, to be reduced by carbon monoxide, should be in the condition ofsteam. Thus, the liquid water remaining from the pulverized emulsion,that is, that which was not vaporized during flashing, corresponds to,for example, around 90% of the water of the emulsion, to be evaporated,presents the following thermal balance:

    H.sub.2 O(t)→H.sub.2 O(v) ΔH=+539 kcal/kg of H.sub.2 O

Heat required for this vaporization is provided by the exotherms frompartial combustion and reduction reactions occurring at the flameforming region. As the water is being vaporized, it becomes reduced bystoichiometric quantities of CO obtained from partial combustion of thefuel oil mist during flashing, with successive formation of hydrogen,which will next be oxidized by oxygen from atmospheric air, producingnew quantities of steam in the condition of gas at flame temperature.These reduction and oxidation reactions occur in chains until all thewater contained in the emulsion has reacted, and the final product ofthe chemical process is limited to steam gas and carbon dioxide. As fromthis point, all the process becomes physical.

The great amounts of heat obtained are transmitted to the heat receptionsystem by radiation forced convection and conductions, heat exchangefurther occuring between steam-gas and carbon dioxide. Through theutilization of known measuring methods, it has been established that theflame temperature when burning an aqueous emulsion with a first oil, ata given flow rate considered only for the moiety of oil contained in theemulsion, is at least equal to the flame temperature in conventionalburning of a higher flow of the referred first oil, considering theperformance achievement of the two burning processes (emulsion and firstoil) under the same conditions and by the same equipment. It has thusbeen verified, experimentally, that the burning of a certain amount ofemulsion produces at least the same serviceable heat energy obtainedthrough burning of a larger amount of an oil, identical to the oneutilized in the emulsion.

The experimental establishment mentioned above allows us to concludethat a relative energetic gain exists, with burning the referredemulsion, the energetic gain being resultant from an increasedavailability of free H₂ for the combustion reaction (oxidation) which isstrongly exothermic, free H₂ coming from the water portion of theemulsion, through the reduction reaction of flashing water and theremaining water (vaporized) by carbon monoxide resultant from thepartial initial combustion of the emulsion's fuel oil.

The larger availability of free H₂ during the combustion process may beassociated, in terms of relative heat energy gain, to the fact that afuel oil presents a net heat value (NHV), which will be so much largerthe more saturated is its molecule, that is, the larger thehydrogen/carbon ratio in its molecule is.

Thus, when burning the emulsion, the result obtained, in terms ofenergetic yield, is comparable to the one obtained through isolatedburning of another hypothetical fuel oil, containing a higherhydrogen/carbon ratio in its molecule.

From what has been revealed, it is understood that the proposed processis so much more effective, the more unsaturated is the fuel oil utilizedin the emulsion, a situation which occurs with fuel oils supplied byBrazilian refineries.

Further to the basic technical effect mentioned above and related to theobtention of a determined heat yield, through lower consumption of anunsaturated fuel oil it can further be established that the NHV yield ofthe aqueous emulsion with the mentioned first unsaturated fuel oil, ishigher than the NHV of another fuel oil presenting the same carbonicchain as the first, however, saturated, according to technicalliterature.

It is understood that the fact commented above comes from the additionalconsumption of energy to dissociate the carbon-hydrogen bonds of thesaturated molecules of another fuel oil. The saturated molecules of fueloil present a higher NHV than the ones of unsaturated molecules. Duringa conventional process of burning saturated fuel oil, part of the energyproduced is consumed to dissociate hydrogen-carbon links of the oilmolecules.

In the case of conditions and reactions to which the emulsion issubmitted, one is able to obtain energetic gain related to theavailability of an amount of hydrogen in the burning process,corresponding to the one obtained with a corresponding saturated fueloil, without the need to expend energy for dissociation of thecarbon-hydrogen links of the saturated oil molecule, additional to thoseexisting in the said first unsaturated oil used in the emulsion of theprocess in question.

To those skilled in the art, reading this process should reveal theapplication of the same to burning other unsaturated oils, includingrenewable ones, such as by-products from bio-digestors or from thealcohol-sugar industry and others, not constituting, however, impairmentto the inventiveness demonstrated by the process, as exposed.

Finally, as may be observed, the proposed hydro-oily emulsion burningprocess further to its high heat yield, presents an extremely clean burnin terms of particulate matter, since the conversion of fuel oil intocarbon dioxide and steam-gas is practically total, thus it should beconsidered as an important contribution of technology to thepreservation of environment.

The process, due to containing water, will further permit itsassociation to other technologies to control polution generated byNo_(x), SO₂ and SO₃, or the like.

The following non-limiting example illustrates the improved performanceof the proposed process, in comparison to a conventional fuel-oilburning process:

                  TABLE    ______________________________________               HIDROL  FUEL OIL  REMARKS    ______________________________________    Steam production                 4713      4698      --    Kg/hour    Oil Consumption                 237,8     330,3     Fuel-Oil    Kg/hour                          savings 28%    Net Heat Produced                 2,62      2,68      Titre    Mcal/hour                        considered                                     for each case    Particulate Emission                 0,537     2,5       -78,5%    Kg/hour    Specific Emission                Reduction    SO.sub.x.KgSO.sub.x /Mcal                 0,438     0,575      23,8%    (net)    Particulate specific                 205,0     932,0        78%    Emission Grams/Mcal    (net)    ______________________________________     Specification and Equipment     Tubular fire boiler (supplier: Pontin)     Nominal Steam Production: 5.000 Kg/hr.     Gauge Working Pressure: p = 10 Bar     Fuel: Fuel Oil (Net Heat Value = 9.650 Kcal/Kg: Viscosity = 70 cst @     100° C.)     Burner: mechanical pressure (supplier: Coen)     Remarks:     1) Fuel Oil and Hidrol burning tests were effected under same conditions.     2) the values shown represent an average of measurements effected during     36 consecutive hours, for both burning tests.     3) Characteristics of the emulsion:     3.1 weight percent of oil: 64%     3.2 pressure of the emulsion at the burner for pulverization: 10 Bar     3.3 temperature of the emulsion at the burner for pulverization:     120° C.     4) Characteristics of the fueloil:     4.1 pulverization pressure: 10 Bar     4.2 pulverization temperature: 130° C.     5) Particulates collected according to EPA procedures.

We claim:
 1. Hydro-oily emulsion burning process characterized in thatit comprises the steps of:emulsifying and aerating the water and thefuel oil, by means of agitation in a mixing tank, the water beingmaintained at a minimum temperature of 20° C.±2° C. and the fuel oil ata maximum temperature lower than that of vaporization of water and at anadequate working pressure to facilitate the desired emulsification, theconcentration of water in the emulsion being calculated to reactstoichiometrically during combustion, producing hydrogen and carbondioxide, said emulsion being maintained at a temperature sufficient topermit an interfacial tension between fuel oil and water and air atcompatible levels to stabilize the emulsion and at a pressurecorresponding to a temperature of saturated water steam substantiallyhigher than the temperature of the emulsion, so that the saturated watersteam presents all the water maintained in the form of droplets ofaround 1 to 10 microns uniformly dispersed, together with micro bubblesof air, in the fuel oil, the speed and time of agitation beingdetermined in order that the aerated emulsion obtained presents aspecific gravity around 20%±5% lower than the deaerated hydro-oilyemulsion; stabilizing the aerated emulsion in a rest tank, maintainedunder temperature and pressure condition that ensure the required ratioof interfacial tension between water and oil and maintenance of thewater concentration, for a period of time required and sufficient topractically fully deaerate said emulsion: conducting the deaerated andstabilized emulsion to a burner nozzle, maintaining the emulsionconduction temperature between a maximum value corresponding to that asaturated steam pressure mandatorily lower than the emulsion conductionpressure and a minimum value corresponding to the minimum sensible heatstored capable of vaporizing a minimum quantity of water under an abruptpressure drop condition, the pressure of conduction of the emulsionbeing maintained within the operating values required by the burner;pulverizing the emulsion through the burner, in uniform particles ofaround 20 to 150 microns, each particle comprising a plurality of saidwater droplets in the emulsion, surrounded by a film of oil, saidpulverization being effected so as to provoke an abrupt depressurizationof the emulsion, sufficient to cause the instantaneous vaporization ofpart of the water from the droplets and the consequent disintegration ofthe particles of the pulverized emulsion, said pulverization beingeffected in an environment sufficiently poor of air in order to avoiddirect formation of carbon dioxide and to convey the followingreactions:a. partial combustion of the fuel oil with part of an amountof oxygen introduced in the pulverization environment, forming carbonmonoxide and releasing heat; b. reduction of water vaporized during theabrupt depressurization of the emulsion, by means of a stoichiometricamount of part of the referred carbon monoxide, forming carbon dioxideand hydrogen and releasing heat;c. oxidation of hydrogen, from reactionb, with the remaining oxygen available in the pulverization environment,forming hiperheated water steam at burner flame temperature; d.vaporization of water, remaining in the droplets, by the heat producedin reactions a and b; e. reduction of water vaporized in reaction d bythe carbon monoxide remaining from step a, through chain reactionsidentical to reactions b and c, in order to provoke total combustion ofthe oil.
 2. Process, according to claim 1, characterized in that thefuel oil is pre-heated to a temperature of around 50° C. to 200° C. 3.Process, according to claim 1, characterized in that the emulsificationis performed through mechanical agitation at around 700 r.p.m., duringperiods of around 2 to 3 minutes.
 4. Process, according to claim 1,characterized in that the emulsion temperature, after beating, ismaintained between around 70° to 90° C. in a non pressurized mixingtank, or above 90° C. in a pressurized tank.
 5. Process, according toclaim 1, characterized in that the hydro-oily emulsion presents around55% to 70% fuel oil.
 6. Process, according to claim 1, characterized inthat the stabilization and deaeration stage of the emulsion is performedat a temperature of around 70° C. to 90° C.
 7. Process, according toclaim 1, characterized in that the stabilization and deaeration stage isperformed during a period of time varying between around 6 and 12 hours.8. Process, according to claim 1, characterized in that the conductiontemperature is, at most, corresponding to a pressure of water saturatedsteam around 15% lower than the emulsion conduction pressure. 9.Process, according to claim 8, characterized in that the conductiontemperature of the emulsion to the burner nozzle ranges between around120° C. and 250° C.
 10. Process, according to claim 1, characterized inthat around 10% of the water from the pulverized droplets are instantlyvaporized by flashing.
 11. Process, according to claim 1, characterizedin that the partial combustion of fuel oil and reduction of gasifiedwater by flashing occur at the ignition temperature of fuel oil. 12.Process, according to claim 1, characterized in that the water steamformed in the reaction of hydrogen oxidation, resulting from thereaction of reduction of water steam by flashing, presents itself at theburner flame temperature.